Apparatus for contacting solid particles with gaseous fluids



June 17, 1947. B. B. RUSSELL, 3D 2,422,262

APPARATUS FCR CONTACTING SOLID PARTICLES WITH GASEOUS FLUIDS AFiled Aug. 2, 1944 3 Sheets-Sheet l arreb Elussell 3rd. 'Saver-:bor

3 Sheets-Sheet 2 B. B. RUSSELL, 3D

Filed Aug. 2, 1944 APPARATUS FOR CONTACTING SOLID PARTICLES WITH GASEOUS FLUIDS June 17, 1947,

F I G. 2

arre b. Russel?, 3rd. 'nvenbor u C n r o u .u a

June 17, 1947. B, B RUSSELL, 3D 2,422,262

PPARATUS FOR CONTACTING SOLID PARTICLES WITH GASEOUS FLUIDS Filed Aug. 2, 1944 3 ySheets-.Sheet 5 FIG-5 barreb Russell 3rd., 'Savenbor Qbborneq Patented June 17, 1947 APPARATUS FOR CONTACTING SOLID PARTICLES WITH GASEOUS FLUIDS Barrett B. Russell, 3d, Elizabeth, N. J.,

assignor to Standard Oil Development Company, a corporation of Delaware Application August 2,- 1944, Serial No. 547,665

This invention relates to contacting solid particles in subdivided form with gaseous iiuids, and more particularly, relates to the stripping oi' spent or contaminated catalyst or contact particles following a hydrocarbon catalytic conversion operation.

In the catalytic cracking of hydrocarbons, it is known that coke or carbonaceous material is deposited on the catalyst particles and the catalyst or contact particles must be regenerated as by burning with air to remove the coke or' carbonaceous deposits. Associated with the spent or contaminated catalyst or contact particles are entrained hydrocarbon vapors and gases. In addition, some hydrocarbon vapors and gases are adsorbed on the adsorbent catalytic or contact material and this adsorbed material may be at least partly removed with a stripping gas such as steam.

In the first units built for the catalytic conversion of hydrocarbons using powdered or subdivided catalyst, the reaction products in vapor i'orm and the catalyst particles are passed overhead from the reaction zone or vessel as a relatively dilute suspension and stripping is not a troublesome problem. In the newer type of unit used in the catalytic cracking of hydrocarbons where the spent or contaminated catalyst par- A ticles are withdrawn from the bottom of the reaction zone in a relatively dense dry fluidized liquid-simulating condition and the catalyst is then stripped, incomplete stripping has Ibeen obtained.

As the spent or contaminated catalyst or contact particles are withdrawn in a dense phase, apparently there is more entrainment of hydrocarbon vapors and gases and more adsorption of hydrocarbon vapors and gases on the catalyst or contact particles. With incomplete stripping,l

more combustible material is added to the regeneration zone and more carbonaceous material must be burned. This results in a higher loss of feed stock as coke or carbonaceous material which is burned in the regeneration zone, and in addition, more heat is generated in the regeneration zone than is required for the process.

According to my invention, the catalyst or contact particles being withdrawn in a dense iluidized dry liquid simulating condition are passed through an annular stripping section or zone below the conversion or cracking zone, the stripping zone or section being subdivided into two or more concentric stripping sections. One or more vertical cylinders or partitions are concentrically arranged in the usual annular strips' claims. (c1. za-zss') ping zone to form two or more annular stripping zones of substantially equal volume.

To further improve the stripping eiiiciency, baille means may be introduced into one or more of the annular stripping zones. Such baille means may be a vertically alternating single annular and two part lannular construction, for

example, but other solids-gas contacting apparatus may be used. With the vertically alterc hating sin'gle annular and two part annular baille construction, agitation and mixing are increased and localized points of high velocity are obtained.

Further improvement in the stripping eillciency may be obtained by injecting the stripping gas perpendicularly away from the faces oi the annular bailies. In this way a transverse flow of stripping gas is obtained through the descending `mass of spent or contaminated catalyst or contact particles. Such stripping may also be used in a single batlled annular stripping section with the cylindrical partition omitted and improved results obtained over the unbaiiled annular stripping section using countercurrent stripping only.

In the drawings:

Fig. 1 represents a vertical longitudinal crosssection of one lform of apparatus adapted to be used in carrying out my invention;

Fig. 2 represents an enlarged vertical longitudinal cross-section of the lower portion of the apparatus shown in` Fig. 1; and

Fig. 3 represents a partial horizontal transverse cross-sectional view taken on line 3-3 of Fig. 2.

Referring now to the drawing, the reference character I0 designates a cylindrical vessel provided with an inlet I2 for introducing gaseous fluid or a mixture of gaseous fluid and catalyst or contact particles in subdivided form. 'I'he gaseous iiuid from line I2 is introduced into the cone I4 arranged in the lower portion of the reaction vessel I 0 and provided with a distribution plate I6 whereby solids and gaseous iiuid are evenly distributed across the area of the reaction vessel.

The velocity of the gaseous iluid is selected to maintain the solid particles in a dry dense iluidized liquid-simulating condition as shown at I8 having a level indicated at 22. The particles are maintained in a turbulent condition and exceedingly good mixing and agitation are obtained.

etc., asufiicient amount of hot generated cata-.-v

lyst being used to vaporize the oil and raise it to conversion temperature.

In the catalytic cracking of hydrocarbons any suitable cracking catalyst may be used as. ,for example, acid-treated bentonite clay, synthetic silica alumina gels, synthetic silica magnesia gels, etc. Preferably the catalyst lis used in powdered form having a size between about 200 and 400 standard mesh but coarser catalyst maybe used if desired. Using acid-treated bentonite clay; or synthetic silica alumina gel in ypowdered form. the density ofthe mixture shown at i8 may vary between about 10 1bs./cu. ft. and 40 lbs./ cu. ft., depending on the velocity of the vapors or gases section 88. The catalyst or contact particles during stripping and vduring passagev through the. strippingv section are maintained in a relatively dense d ry uidized liquid-simulating condition.

The stripped particles iiow down into the conical bottom lportion 82 of the reaction vessel III and are collected therein as a dense viiuidized mixture shown at 63 from which they pass to a standpipe- 64. Only a portion of the standpipe is shown in. Fig. l. The stripped particles are maintained in a dense iluidized condition in the passing upwardly through the mixture or' bed I8.

'I'he yvelocity may range between about 1/2 ft./sec

ond and 2 ft./second, the lower velocities giving f higher densities in the bed or mixture I8.

Above the dense bed or mixture I8 is a dilute phase in which the gaseous duid or reaction products in vapor form contain only a small amount of entrained catalyst or contact particles.

The gaseous uid from the dilute phase 24 is passed through inlet 26 of al separating-means 26 arranged in the upper portion of the reaction vessel I0. The separating means 28 separates most of the entrained catalyst or contact particles from the gaseous uid passing upwardly through the reaction vessel i0. .The separated catalyst or contact particles are returned to the dense bed or mixture I8 through line 28 which standpipe to produce a hydrostatic pressure at thebase of the standpipe which is suillciently 'high to move the stripped vspentcatalyst particlesvto an air stream which carries the catalyst -to a regeneration rone (not shown).

Referring now to Fig. 2 of the drawing, it will be seen that myl improved stripping section 38 includes va cylindrical baille or partition 68 which is concentric'with the apron or skirt 42 and with the wall of the reaction vessel l0. The cylindrical baille or partition 6-8 subdivides the annular stripping section into two smaller annular stripping sections 12 and-14 which are concentrically arranged. Nozzles 64 feed stripping gas into lsection 14 and nozzles 56 feed stripping gas into dips below the level 22 in the reaction vessel i8.

The gaseous iluid or vaporous reaction products leave the top of the reaction vessel i0 through 'line 32 and maybe passed to any suitable equipment for recovering desired products. Inthe catalytic cracking of hydrocarbons the cracked vaporous products are preferably passed to a fractionating tower to separate gasoline from gases and higher boiling hydrocarbons. The sep- V arating means is shown in the drawing as a cy clone separator but other separating means may be used as. for example, a Multiclone separator.

During the catalytic cracking or conversion of hydrocarbons, the catalyst orl contact particles become contaminated or spent by the deposition on the particles of coke or carbonaceous material. vThis carbonaceous or combustible material must be removed before the catalyst is used over again in another cracking or conversion operation. The contaminated or spent catalyst or contact particles are withdrawn from the bottom of the dense bed or mixture I8 and passed downwardly through a stripping or purging section generally indicated at 88.

The usual purging section is annular in form and is formed by the inner wall of the vessel I0 and a skirt or apron 42, which descends from the distribution plate I6. The bottom of the apron or skirt 42 may be closed as shown by coneshaped bottom 44 to eliminate any possibility of pockets forming between the feedcone inlet I4 and the skirt or apron 42. My invention comprises an improved stripping or purging section and will be presently described in connection with the detailed view shown in Fig. 2.

Stripping gas, such as steam, superheated to `about 250 F. to 1100" F. is introduced through line 46 and passed through annular distributing 70 lines 48 and 52 into the bottom portion of the stripping section 38. Line 88 is provided with fnozzles 64 and line 52 is provided with nozzles r66 for introducing the stripping gas at a plurality section 12. The cylindrical partition or baiie 68 is so positioned that the volumes of the stripping sections 12 and 14 are substantially equal. The

two stripping sections 12 and 14 give better stripping than the same stripping section with the cylindrical partition or baille 68 removed.

In order to further improve stripping, I have included a baiile constructionl in each of the smaller stripping sections. Such baille construction in the vertical section shown in Figs. 1 and 2 resembles a disc and doughnut construction and the baille construction shown functions in a way similar to a disc and doughnut baille conf struction. As the stripping section is annular, the elements of the baille construction are also annular as will be seen from an inspection of Figs. 2 and 3.' One portion of the top two-part baille is shown at 16, the element being triangular in cross-section with the base thereof secured to the apron or skirt 42 and the remaining faces 18 and 82 coming to an apex at 84. The element 16 is arranged in the upper part of the stripping sectionv 12.

The other portion of the top two-part baille is shown at 88 and from the drawing it will be seen that it is similar in construction to the other- 'I'he apex 84 of the one baille section 16 and the apex 89 of the other baille section 88 arev directed toward each other and form a narrower annular passageway 90 in the stripping section 12. As the dense mixture to be stripped passes through the narrowed passageway 90, there is increased agitation and a higher velocity of the stripping gas so that improved stripping is obtained.

Arranged below the two-part baille construction 16, 88 is a single annular baille 92 which is substantially triangular in cross-section and has a pointed top or apex 94 and diverging sides 96 and 98. The bottom of the. baille 92 is sho-waas curved at |02 but may be a straight line. The apex 94 is arranged at the top of the baille directly beneath the narrowed passageway -9i) above described so that the dense mixture is divided into two streams as it passes downward over the baille l92. The 'bottom portion of the baille 92 forms narrowed passageways |03 adjaof points into the bottom portion of the stripping cent the bottom |02 of the baie 82 and here again, increased agitation and higher velocities are obtained.

Arranged below the baffle 92 is another twopart baille construction comprising elements |04 and |06 which are similar in construction to the two-part baiile construction 16, 88 above described. Arranged below the baille construction |04, |06 is another single annular bafile construction |08 which is similar to the baille 92 above described.

The other stripping section 14 is provided with a top two-part bafiie construction ||2, H4 which is similar in construction to the two-part baille construction 16, 88 above described. Below this baille construction ||2, ||4 is a single annular baille ||6 which is similar to the baffle 92 above described. Below the baffle ||'6 is another twopart baille construction ||8 and |22which is similar to the two-part baille construction 16, 88 above described. Below the two-part baille construction ||8, |22 is another single annular baille |24 similar to the baille 92 above described.

While I have described my improved stripping section as being formed Iby subdividing, the usual stripping section into two smaller concentric stripping sections, it is to be understood that more than one concentric cylindrical fbaiile may be used to subdivide the usual vstripping section into a plurality of smaller concentric stripping sections. Such 'smaller stripping sections give improved stripping, over the usual single annular stripping section. stripping is further improved byvinciudingfV the baffle construction above described including Athe two-part -baiiles and the single annular bafiles.

The nozzles for introducing stripping gas have Ibeen shown at 54 and 56 and preferably the nozzles yare arranged around the bottom of the stripping section so that'stripping gas is introduced into the bottom portion of each of the separate' stripping portions 12'and 'I4 around the entire bottom of each section.

If desired, the stripping eiiiciency in the separate stripping sections may be further increased by introducing a stripping gas perpendicularly 4away from the face of the lbaiies. This is shown in Fig. 2 in connection with one section of the two-part baille construction but may be used on any number of such baffles desired. As shown in Fig. 2, an inlet line |28 is provided with branch lines |30 which direct the stripping gas ,perpendicularly to the slanting side |32 of the baiiie construction 04. With such stripping the stripping gas passes at right angles to the downilowing mixture to be stripped andbetter stripping is obtained.

the stripping gas may The stripping gas may comprise superheated steam or other inert gases such as carbon dioxide, nitrogen, etc., also recycle gas, CH4, C21-Is, CsHa, H2, C4H1o.

In the catalytic cracking of hydrocarbons, the temperature in the reaction vessel I0 may vary between about 850 and 1100 F. but different temperatures may lbe used for other hydrocarbon conversion operations or other processes involving chemical reactions. The catalyst to oil ratio may vary between about 5 to 1 to 35 to 1 by weight.

The velocity of the stripping gas passing upwardly zthrough the separate stripping sections is so selected that the downowing mixture is maintained in a relatively dense fluidized condition. While there may beportions of the mixture of lighter density, the average density of the fluidized mixture passing through the striphydrocarbons, it is to ping zones when using synthetic silica alumina powdered catalyst may vary between about 10 lbs/cu. ft. and 30 lbs/cu. ft. 'I'he velocity of Ibe between about 0.1 ft./second to 1.5 ft./second, preferably about 0.3 ft./second to 0.6 ft./second.

To determine the stripping eiiiciency, a screen sampling device is used which allows separation of the hot vapors from the catalyst followed by condensation and separation of the gaseous components at atmospheric conditions. Oil and water are condensed and gas is metered. Perfect stripping would show only water. No stripping would show gas and oil, no Water. Using myv invention, the efciency of the stripping step can be increased to about to 100%. This means that about'95 to 100% of the condensible hydrocarbons obtained in the above step are removed during stripping.

'I'he hydrocarbon constituents which are removed during the stripping step are passed upwardly into the dense bed or mixture I8 in the reaction vessel I0 and are recovered with the products passing overhead through line 32.

'Ihe following data show that increased strip` ping etliciency is obtained when using smaller diameter stripping sections or sections having a smaller cross-sectional area, but the same length. The catalyst flow density in each case is 275 lbs./sq.ft./min.

6" unbaled stripper Relative velocity (feet/sec.) of the gas with respect to the .While my invention has been specifically described in connection with catalytic cracking of be understood that it is also useful in other operations where it is desired to remove a volatile material from spent or contaminated catalyst or contact particles in other reactions. My invention is not to be limited to the specic conditions nor to the specific process described as these are given by way of illustration only and various changes and modiiications may be made without departing from the spirit of my invention.

vI claim:

1. An 'apparatus of the character described including a cylindrical vessel, a centrally arranged circular distribution perforated plate in the lower portion of said vessel, means for introducing gaseous uid into said vessel for passage upwardly through said plate, a skirt depending from the perimeter ofsaid plate and concentric with said plate and said vessel, a cylindrical l"baille concentric with the wall of said vessel and with said skirt whereby a plurality of annular concentric zones are formed, means for introducing a gaseous uid into said annular zones, said vessel being adapted to contain a dense dry fluidized liquid-simulating mixture of contact particles and gaseous uid which mixture passes down through said annular zones wherein the contact particles are mixed with the gaseous i'luid introduced into said annular zones.

2. An apparatus according to claim 1 wherein baille means are provided in at least one oi' said annular zones whereby better contact is obtained between the contact particles and gaseous fluid.

3. An apparatus according to claim 1 wherein baille means are provided in at least one of said annular zones whereby better contact is obtained between the contact particles and gaseous iiuid and means are included adjacent said baille means to inject gas transversely of the downward flow of dense mixture through at least one of said annular zones.

4. In an apparatus of the character described including a cylindrical vessel, acircular distribution perforated plate centrally arranged in the lower portion of said vessel, means for introducing gaseous fluid into said vessel for passage upwardly through said plate, a skirt depending from the perimeter of said plate and concentric with said plate and said vessel, the improvement including a cylindrical baille concentric with the wall of said vessel and with said skirt to subdivide the zone between said skirt and said wall into a plurality of annular concentric zones, means for introducing a gaseous fluid into each of said annular zones, said vessel being adapted to contain a dense dry tluidized liquid-simulating mixture of contact. particles and gaseous uid which mixture passes down through said annular zones wherein the contact particles are mixed with the gaseous fluid introduced into said annular zones.

5. An apparatus according to claim 4 wherein baille means are provided in at least one of said annular zones whereby better contact is obtained between the contact particles and gaseous fluid.

6.l An apparatus according to claim 4 wherein said cylindrical baille is so placed that the annular concentric zones have substantially the same volume.

7. An apparatus of the character described including a cylindrical' vessel, a circular distribution perforated plate centrally arranged in the lower portion of said vessel, means for introducins gaseous fluid into said vessel. an annular chamber adjacent said plate and concentric therewith, a cylindrical baille concentric 'with the wall of said vessel and with said plate subdividing said annular chamber into a plurality of annular concentric zones, means for introducing a gaseous fluid into the bottom portion of each of said annular zones, said vessel being adapted to contain a dense dry fiuidized liquidsimulating mixture of contact particles and gaseous iiuld which mixture passes down through said annular concentric zones wherein the contact particles are mixed with the gaseous fluid introduced into said annular zones.

8. An apparatus according to claim 'l wherein baille means are provided in at least one of said annular zones whereby better contact is obtained between the contact BARRETT B. RUSSELL', 31u.

REFERENCES CITED The following references are of record in the file of this patent:

UNITED STATES PATENTS Date particles and gaseous fluid. 

